U.S. patent application number 15/472516 was filed with the patent office on 2018-10-04 for method and device for direct-contact heat exchange between a fouling liquid and a cooling fluid.
The applicant listed for this patent is Larry Baxter, Stephanie Burt, Nathan Davis, Christopher Hoeger, Eric Mansfield, Kyler Stitt. Invention is credited to Larry Baxter, Stephanie Burt, Nathan Davis, Christopher Hoeger, Eric Mansfield, Kyler Stitt.
Application Number | 20180283809 15/472516 |
Document ID | / |
Family ID | 63669127 |
Filed Date | 2018-10-04 |
United States Patent
Application |
20180283809 |
Kind Code |
A1 |
Baxter; Larry ; et
al. |
October 4, 2018 |
Method and Device for Direct-Contact Heat Exchange between a
Fouling Liquid and a Cooling Fluid
Abstract
A device and a method for conducting a heat exchange process is
disclosed. A direct-contact heat exchanger is provided comprising a
process inlet, a coolant inlet, and an interior surface. A process
stream is provided to the process inlet to be cooled in the heat
exchange process by direct contact with a coolant stream that is
provided to the coolant inlet. The coolant stream comprises a
liquid or a gas. The heat exchange process comprises a phase change
from liquid to gas, a sensible heat transfer, or a combination
thereof. The cooling process leads to chemical reactions, solids
formation in the bulk phase, or a combination thereof. The use of
the direct-contact heat exchanger minimizes such reactions on the
interior surface. In this manner, the heat exchange process is
conducted.
Inventors: |
Baxter; Larry; (Orem,
UT) ; Hoeger; Christopher; (Provo, UT) ; Burt;
Stephanie; (Provo, UT) ; Mansfield; Eric;
(Spanish Fork, UT) ; Stitt; Kyler; (Lindon,
UT) ; Davis; Nathan; (Bountiful, UT) |
|
Applicant: |
Name |
City |
State |
Country |
Type |
Baxter; Larry
Hoeger; Christopher
Burt; Stephanie
Mansfield; Eric
Stitt; Kyler
Davis; Nathan |
Orem
Provo
Provo
Spanish Fork
Lindon
Bountiful |
UT
UT
UT
UT
UT
UT |
US
US
US
US
US
US |
|
|
Family ID: |
63669127 |
Appl. No.: |
15/472516 |
Filed: |
March 29, 2017 |
Current U.S.
Class: |
1/1 |
Current CPC
Class: |
F28F 19/00 20130101;
F28C 3/06 20130101; F28F 19/006 20130101; F28C 3/04 20130101; F28C
3/08 20130101; F28C 3/12 20130101 |
International
Class: |
F28F 19/00 20060101
F28F019/00; F28C 3/04 20060101 F28C003/04; F28C 3/06 20060101
F28C003/06; F28C 3/08 20060101 F28C003/08; F28C 3/12 20060101
F28C003/12 |
Goverment Interests
[0001] This invention was made with government support under
DE-FE0028697 awarded by The Department of Energy. The government
has certain rights in the invention.
Claims
1. A method for conducting a heat exchange process comprising:
providing a direct-contact heat exchanger comprising a process
inlet, a coolant inlet, and an interior surface; and, providing a
process stream to the process inlet to be cooled in the heat
exchange process by direct contact with a coolant stream that is
provided to the coolant inlet, the coolant stream comprising a
liquid or a gas, wherein the heat exchange process comprises a
phase change from liquid to gas, a sensible heat transfer, or a
combination thereof, and the cooling process leads to chemical
reactions, solids formation in a bulk phase, or a combination
thereof, the use of the direct-contact heat exchanger minimizing
such reactions on the interior surface; whereby the heat exchange
process is conducted.
2. The method of claim 1, wherein the cooling stream comprises a
liquid refrigerant that vaporizes by contact with the feed liquid,
a gas refrigerant, or a combination thereof.
3. The method of claim 1, wherein the coolant inlet comprises a
pressure-drop device and the cooling stream, comprising a liquid
refrigerant, is vaporized by passing through the pressure drop
device into the direct-contact heat exchanger, and wherein the
pressure-drop device comprises a valve, turbine, nozzle, orifice,
or combinations thereof.
4. The method of claim 1, wherein solids formation in the bulk
phase produces solid carbon dioxide, solid nitrogen oxide, solid
sulfur dioxide, solid nitrogen dioxide, solid sulfur trioxide,
solid hydrogen sulfide, solid hydrogen cyanide, water ice, solid
hydrocarbons, precipitated salts, or combinations thereof.
5. The method of claim 1, wherein the process stream comprises
soot, dust, minerals, microbes, wastewater, acids, bases,
immiscible liquids, paper pulp, metal hydrides, solid carbon
dioxide, solid nitrogen oxide, solid sulfur dioxide, solid nitrogen
dioxide, solid sulfur trioxide, solid hydrogen sulfide, solid
hydrogen cyanide, water ice, solid hydrocarbons, precipitated
salts, other sulfides, other sulfates, chlorides, or combinations
thereof.
6. The method of claim 1, wherein the direct-contact heat exchanger
comprises a spray tower, bubble contactor, mechanically agitated
tower, or combinations thereof.
7. The method of claim 1, wherein the coolant inlet comprises a gas
distributor, bubble plate, sparger, nozzle, or combinations
thereof.
8. The method of claim 1, wherein the coolant stream is soluble in
the process stream, the process stream is pre-cooled to produce a
pre-chilled process stream, and the coolant stream is less soluble
in the pre-chilled process stream.
9. The method of claim 8, wherein a temperature of the pre-chilled
process stream is near a freezing point of the pre-chilled process
stream.
10. The method of claim 8, wherein a portion of the coolant stream
is dissolved into the product stream and the process stream is
further cooled to near a freezing point of the process stream,
causing the coolant stream to become insoluble in the process
stream, whereby the process stream is removed.
11. A direct-contact heat exchanger comprising: a process inlet, a
coolant inlet, and an interior surface, wherein: a process stream
is provided to the process inlet to be cooled and a coolant stream
is provided to the coolant inlet to cool the process stream by
direct contact, the coolant stream comprising a liquid or a gas;
the coolant stream cools the process stream by a cooling process
comprising a phase change from liquid to gas, a sensible heat
transfer, or a combination thereof; the cooling process leads to
chemical reactions, solids formation in a bulk phase, or a
combination thereof, the use of the direct-contact heat exchanger
minimizing such reactions on the interior surface.
12. The device of claim 11, wherein the cooling stream comprises a
liquid refrigerant that vaporizes by contact with the feed liquid,
a gas refrigerant, or a combination thereof.
13. The device of claim 11, wherein the coolant inlet comprises a
pressure-drop device and the cooling stream, comprising a liquid
refrigerant, is vaporized by passing through the pressure drop
device into the direct-contact heat exchanger, and wherein the
pressure-drop device comprises a valve, turbine, nozzle, orifice,
or combinations thereof.
14. The device of claim 11, wherein solids formation in the bulk
phase produces solid carbon dioxide, solid nitrogen oxide, solid
sulfur dioxide, solid nitrogen dioxide, solid sulfur trioxide,
solid hydrogen sulfide, solid hydrogen cyanide, water ice, solid
hydrocarbons, precipitated salts, or combinations thereof.
15. The device of claim 11, wherein the process stream comprises
soot, dust, minerals, microbes, solid carbon dioxide, solid
nitrogen oxide, solid sulfur dioxide, solid nitrogen dioxide, solid
sulfur trioxide, solid hydrogen sulfide, solid hydrogen cyanide,
water ice, solid hydrocarbons, precipitated salts, or combinations
thereof.
16. The device of claim 11, wherein the direct-contact heat
exchanger comprises a spray tower, bubble contactor, sieve tray
column, bubble tray column, baffle tray column, mechanically
agitated tower, perforated pipe, air-sparged hydrocyclone,
nozzle-injected hydrocyclone, or combinations thereof.
17. The device of claim 11, wherein the coolant inlet comprises a
gas distributor, bubble plate, sparger, nozzle, or combinations
thereof.
18. The device of claim 11, wherein the coolant stream is soluble
in the process stream, the process stream is pre-cooled to produce
a pre-chilled process stream, and the coolant stream is less
soluble in the pre-chilled process stream.
19. The device of claim 18, wherein a temperature of the
pre-chilled process stream is near a freezing point of the
pre-chilled process stream.
20. The device of claim 18, wherein a portion of the coolant stream
is dissolved into the product stream and the process stream is
further cooled to near a freezing point of the process stream,
causing the coolant stream to become insoluble in the process
stream, whereby the process stream is removed.
Description
FIELD OF THE INVENTION
[0002] This invention relates generally to the field of
direct-contact heat exchange. More particularly, we discuss the
process of direct contact heat exchange between fouling or
corrosive liquids and cooling fluids.
BACKGROUND
[0003] The art of direct-contact heat exchange has been a part of
the human experience since the discovery of cooking. More recently,
direct-contact heat exchange is used in industry for warming and
cooling gases, liquids, and solids. Direct-contact heat exchange is
designed to maximize the contact surface area between the media
exchanging heat. In general, this goal is accomplished by
maximizing the amount of solid surface area of the exchanger.
However, when the heat exchange process produces solids that can
foul the flow paths of the exchanger, or reactive intermediates
that can corrode or otherwise react with the surface of the
exchanger, maximization of exchanger surface area is
counter-productive. No effective system or method for conducting
heat exchange of these fouling and reactive liquids is
available.
[0004] U.S. Pat. No. 3,496,996 to Osdor teaches an apparatus for
providing large surface area direct contact between a liquid and
another fluid. The surface area of the exchanger is maximized to
provide the most surface exchange between a liquid and a fluid. The
present disclosure differs from this disclosure in that the amount
of contact with the exchanger itself is maximized, rather than
minimized. This disclosure is pertinent and may benefit from the
methods disclosed herein and is hereby incorporated for reference
in its entirety for all that it teaches.
[0005] U.S. Pat. No. 3,988,895 to Sheinbaum teaches power
generation from hot brines. A multi-tray exchanger is utilized that
maximizes heat exchange with the brine. The present disclosure
differs from this disclosure in that the amount of contact with the
exchanger itself is maximized, rather than minimized, in spite of
the brine solution in use. This disclosure is pertinent and may
benefit from the methods disclosed herein and is hereby
incorporated for reference in its entirety for all that it
teaches.
SUMMARY
[0006] A device and a method for conducting a heat exchange process
is disclosed. A direct-contact heat exchanger is provided
comprising a process inlet, a coolant inlet, and an interior
surface. A process stream is provided to the process inlet to be
cooled in the heat exchange process by direct contact with a
coolant stream that is provided to the coolant inlet. The coolant
stream comprises a liquid or a gas. The heat exchange process
comprises a phase change from liquid to gas, a sensible heat
transfer, or a combination thereof. The cooling process leads to
chemical reactions, solids formation in the bulk phase, or a
combination thereof. The use of the direct-contact heat exchanger
minimizes such reactions on the interior surface. In this manner,
the heat exchange process is conducted.
[0007] The cooling stream may comprise a liquid refrigerant that
vaporizes by contact with the feed liquid, a gas refrigerant, or a
combination thereof. The coolant inlet may comprise a pressure-drop
device and the cooling stream, comprising a liquid refrigerant, is
vaporized by passing through the pressure drop device into the
direct-contact heat exchanger. The pressure-drop device may
comprise a valve, turbine, nozzle, orifice, or combinations
thereof.
[0008] Solids formation in the bulk phase may produce solid carbon
dioxide, solid nitrogen oxide, solid sulfur dioxide, solid nitrogen
dioxide, solid sulfur trioxide, solid hydrogen sulfide, solid
hydrogen cyanide, water ice, solid hydrocarbons, precipitated
salts, or combinations thereof.
[0009] The process stream may comprise soot, dust, minerals,
microbes, wastewater, acids, bases, immiscible liquids, paper pulp,
metal hydrides, solid carbon dioxide, solid nitrogen oxide, solid
sulfur dioxide, solid nitrogen dioxide, solid sulfur trioxide,
solid hydrogen sulfide, solid hydrogen cyanide, water ice, solid
hydrocarbons, precipitated salts, other sulfides, other sulfates,
chlorides, or combinations thereof.
[0010] The direct-contact heat exchanger may comprise a spray
tower, bubble contactor, mechanically agitated tower, or
combinations thereof.
[0011] The coolant inlet may comprise a gas distributor, bubble
plate, sparger, nozzle, or combinations thereof.
[0012] The coolant stream may be soluble in the process stream,
with the process stream pre-cooled to produce a pre-chilled process
stream, and the coolant stream thus less soluble in the pre-chilled
process stream. A temperature of the pre-chilled process stream may
be near a freezing point of the pre-chilled process stream. A
portion of the coolant stream may be dissolved into the product
stream and the process stream further cooled to near a freezing
point of the process stream, causing the coolant stream to become
insoluble in the process stream, whereby the process stream is
removed.
BRIEF DESCRIPTION OF THE DRAWINGS
[0013] In order that the advantages of the invention will be
readily understood, a more particular description of the invention
briefly described above will be rendered by reference to specific
embodiments illustrated in the appended drawings. Understanding
that these drawings depict only typical embodiments of the
invention and are not therefore to be considered limiting of its
scope, the invention will be described and explained with
additional specificity and detail through use of the accompanying
drawings, in which:
[0014] FIG. 1 shows a method for conducting a heat exchange
process.
[0015] FIG. 2 shows a cross-sectional view of a direct-contact heat
exchanger for conducting a heat exchange process.
[0016] FIG. 3 shows a cross-sectional view of a direct-contact heat
exchanger for conducting a heat exchange process.
[0017] FIG. 4 shows a cross-sectional view of a direct-contact heat
exchanger for conducting a heat exchange process.
[0018] FIG. 5 shows a cross-sectional view of a direct-contact heat
exchanger for conducting a heat exchange process.
[0019] FIG. 6 shows a cross-sectional view of a direct-contact heat
exchanger for conducting a heat exchange process.
[0020] FIG. 7 shows an isometric cutaway view of a direct-contact
heat exchanger for conducting a heat exchange process.
DETAILED DESCRIPTION
[0021] It will be readily understood that the components of the
present invention, as generally described and illustrated in the
Figures herein, could be arranged and designed in a wide variety of
different configurations. Thus, the following more detailed
description of the embodiments of the invention, as represented in
the Figures, is not intended to limit the scope of the invention,
as claimed, but is merely representative of certain examples of
presently contemplated embodiments in accordance with the
invention.
[0022] Referring to FIG. 1, a method for conducting a heat exchange
process is shown at 100, as per one embodiment of the present
invention. A direct-contact heat exchanger comprising a process
inlet, a coolant inlet, and an interior surface is provided 101. A
process stream is provided to the process inlet 102 to be cooled in
the heat exchange process by direct contact with a coolant stream
that is provided to the coolant inlet 103. The coolant stream
comprises a liquid or a gas. The heat exchange process comprises a
phase change from liquid to gas, a sensible heat transfer, or a
combination thereof, and the cooling process leads to chemical
reactions, solids formation in the bulk phase, or a combination
thereof. The use of the direct-contact heat exchanger minimizes
such reactions on the interior surface. In this manner, the heat
exchange process is conducted.
[0023] Referring to FIG. 2, a cross-sectional view of a
direct-contact heat exchanger for conducting a heat exchange
process is shown at 200, as per one embodiment of the present
invention. Direct-contact heat exchanger 202 is provided,
comprising process inlet 204, coolant inlet 206, interior surface
208, process outlet 218, and coolant outlet 220. Process stream 210
is provided to process inlet 204. The coolant stream, liquid
refrigerant 212, is provided to coolant inlet 206. Liquid
refrigerant 212 cools process stream 210 to form cooled process
stream 214 by direct contact in a cooling process comprising a
phase change from liquid to gas and a sensible heat transfer,
producing warmed coolant stream 216. The cooling process leads to
chemical reactions, solids formation in the bulk phase, or a
combination thereof. The use of direct-contact heat exchanger 202
minimizes such reactions on interior surface 208. Cooled process
stream 214 leaves through process outlet 218 while warmed coolant
stream 216 leaves through coolant outlet 220.
[0024] Referring to FIG. 3, a cross-sectional view of a
direct-contact heat exchanger for conducting a heat exchange
process is shown at 300, as per one embodiment of the present
invention. Bubble contactor 302 is provided, comprising process
inlet 304, bubble plate 306, interior surface 308, process outlet
318, and coolant outlet 320. Isopentane stream 310 is provided to
process inlet 304, isopentane stream 310 comprising dissolved
carbon dioxide. The coolant stream, liquid nitrogen stream 312, is
provided through bubble plate 306. Liquid nitrogen stream 312 cools
isopentane stream 310 to form cooled isopentane stream 314 by
direct contact in a cooling process comprising a phase change from
liquid to gas and a sensible heat transfer, producing warmed
nitrogen stream 316. The cooling process leads to solid carbon
dioxide formation in the bulk phase. The use of direct-contact heat
exchanger 302 minimizes the production of solid carbon dioxide on
interior surface 308. Cooled isopentane stream 314 leaves through
process outlet 318 while warmed nitrogen stream 316 leaves through
coolant outlet 320.
[0025] Referring to FIG. 4, a cross-sectional view of a
direct-contact heat exchanger for conducting a heat exchange
process is shown at 400, as per one embodiment of the present
invention. Bubble contactor 402 is provided, comprising process
inlet 404, bubble plate 406, interior surface 408, process outlet
418, and coolant outlet 420. Brine stream 410 is provided to
process inlet 404, brine stream 410 comprising dissolved salts. The
coolant stream, liquid methane stream 412, is provided through
bubble plate 406. Liquid methane stream 412 cools brine stream 410
to form cooled brine stream 414 by direct contact in a cooling
process comprising a phase change from liquid to gas and a sensible
heat transfer, producing warmed methane stream 416. The cooling
process leads to precipitation of salts in the bulk phase. The use
of direct-contact heat exchanger 402 minimizes the production of
salts on interior surface 408. Cooled brine stream 414 leaves
through process outlet 418 with the salts entrained, while warmed
methane stream 416 leaves through coolant outlet 420.
[0026] Referring to FIG. 5, a cross-sectional view of a
direct-contact heat exchanger for conducting a heat exchange
process is shown at 500, as per one embodiment of the present
invention. Direct-contact heat exchanger 502 is provided,
comprising process inlet 504, nozzles 506, interior surface 508,
process outlet 518, and coolant outlet 520. Liquid stream 510 is
provided to process inlet 504, liquid stream 510 comprising metal
hydrides. The coolant stream, cold argon stream 512, is provided
through nozzles 506. Cold argon stream 512 cools liquid stream 510
to form cooled liquid stream 514 by direct contact in a cooling
process comprising a sensible heat transfer, producing warmed argon
stream 516. The use of direct-contact heat exchanger 502 minimizes
metal hydrides reacting with or because of interior surface 508.
Cooled liquid stream 514 leaves through process outlet 518, while
warmed argon stream 516 leaves through coolant outlet 520.
[0027] Referring to FIG. 6, a cross-sectional view of a
direct-contact heat exchanger for conducting a heat exchange
process is shown at 600, as per one embodiment of the present
invention. Direct-contact heat exchanger 602 is provided,
comprising process inlet 604, coolant inlet 606, coolant valve 622,
interior surface 608, process outlet 618, and coolant outlet 620.
Slurry stream 610 is provided to process inlet 604, slurry stream
610 comprising solid acid gases. The coolant stream, liquid ethane
stream 612, is provided through nozzles 606. Liquid ethane stream
612 cools slurry stream 610 to form cooled slurry stream 614 by
direct contact in a cooling process comprising a phase change from
liquid to gas and a sensible heat transfer, producing warmed ethane
stream 616. Zoomed in view 624 shows the interface between the
vaporizing ethane stream and slurry stream 610. The use of
direct-contact heat exchanger 602 minimizes deposit of solid acid
gases on interior surface 608. Cooled slurry stream 614 leaves
through process outlet 618, while warmed ethane stream 616 leaves
through coolant outlet 620. Solid acid gases comprise solid forms
of carbon dioxide, nitrogen oxide, sulfur dioxide, nitrogen
dioxide, sulfur trioxide, hydrogen sulfide, and hydrogen
cyanide.
[0028] Referring to FIG. 7, an isometric cutaway view of a
direct-contact heat exchanger for conducting a heat exchange
process is shown at 700, as per one embodiment of the present
invention. Direct-contact heat exchanger 702 is provided,
comprising process inlets 704, coolant inlet 706, interior surface
708, process outlet 718, and coolant outlet 720. Process stream 710
is provided to process inlets 704, process stream 710 comprising
chlorides. Coolant stream 712 is provided through coolant inlet
706. Coolant stream 712 cools process stream 710 to form cooled
process stream 714 by direct contact in a cooling process
comprising a sensible heat transfer, producing warmed coolant
stream 716. The use of direct-contact heat exchanger 702 minimizes
the reaction of chlorides with interior surface 708. Cooled process
stream 714 leaves through process outlet 718, while warmed coolant
stream 716 leaves through coolant outlet 720.
[0029] In some embodiments, the cooling stream comprises a liquid
refrigerant that vaporizes by contact with the feed liquid, a gas
refrigerant, or a combination thereof.
[0030] In some embodiments, the coolant inlet comprises a
pressure-drop device and the cooling stream, comprising a liquid
refrigerant, is vaporized by passing through the pressure drop
device into the direct-contact heat exchanger, and wherein the
pressure-drop device comprises a valve, turbine, nozzle, orifice,
or combinations thereof.
[0031] In some embodiments, solids formation in the bulk phase
produces solid carbon dioxide, solid nitrogen oxide, solid sulfur
dioxide, solid nitrogen dioxide, solid sulfur trioxide, solid
hydrogen sulfide, solid hydrogen cyanide, water ice, solid
hydrocarbons, precipitated salts, or combinations thereof.
[0032] In some embodiments, the process stream comprises soot,
dust, minerals, microbes, wastewater, acids, bases, immiscible
liquids, paper pulp, metal hydrides, solid carbon dioxide, solid
nitrogen oxide, solid sulfur dioxide, solid nitrogen dioxide, solid
sulfur trioxide, solid hydrogen sulfide, solid hydrogen cyanide,
water ice, solid hydrocarbons, precipitated salts, other sulfides,
other sulfates, chlorides, or combinations thereof.
[0033] In some embodiments, the direct-contact heat exchanger
comprises a spray tower, bubble contactor, mechanically agitated
tower, or combinations thereof.
[0034] In some embodiments, the coolant inlet comprises a gas
distributor, bubble plate, sparger, nozzle, or combinations
thereof.
[0035] In some embodiments, the coolant stream is soluble in the
process stream, the process stream is pre-cooled to produce a
pre-chilled process stream, and the coolant stream is less soluble
in the pre-chilled process stream. In some embodiments, a
temperature of the pre-chilled process stream is near a freezing
point of the pre-chilled process stream. In some embodiments, a
portion of the coolant stream is dissolved into the product stream
and the process stream is further cooled to near a freezing point
of the process stream, causing the coolant stream to become
insoluble in the process stream, whereby the process stream is
removed.
[0036] In some embodiments, the coolant inlet comprises a material
that inhibits adsorption of gases, prevents deposition of solids,
or a combination thereof. In some embodiments, this material
comprises ceramics, polytetrafluoroethylene,
polychlorotrifluoroethylene, natural diamond, man-made diamond,
chemical-vapor deposition diamond, polycrystalline diamond, or
combinations thereof.
[0037] In some embodiments, the liquid refrigerant comprises
ethane, methane, propane, R14, nitrogen, oxygen, argon, helium,
xenon, other light gases, aliphatic hydrocarbons, aromatic
hydrocarbons, other refrigerants, or combinations thereof. In some
embodiments, the gas refrigerant comprises ethane, methane,
propane, R14, nitrogen, oxygen, argon, helium, xenon, other light
gases, aliphatic hydrocarbons, aromatic hydrocarbons, other
refrigerants, or combinations thereof.
* * * * *